US2821537A - Catalytic hydrogenation of carbon monoxide with addition of ammonia or methylamine - Google Patents

Description

using these processes.

United States Patent 'Qflice CATALYTIC 'HYDROGENATION F CARBON MONOXEE ADDITION'OF AMMQN-IA 0R METHYLAMINE Walter Rottig, obe'rhausen stei'krade Nord, Germany, assignor to Ruhrchemie Alttieligcslls'chaft, Oberlraus'n- Holten, Germany, and Lurgi G'es'llschaft fu'er Wa'ermetechnik m. b. H.,"Frankfurt am'Main-=Heddernheim, Germany, a German corporation N0 Drawing. Application July 15, 1952 Serial No. 299,000

Claims priority, application Germanyaluly .21, 1951 8 Claims. (Cl. 260-44916) of oxygen-containin g compounds and: preferably alcohols in addition to a'high content of nitrogen-containing compounds and olefins.

Processes for efiecting the catalytic hydrogenation of carbon monoxide with the "addition of ammonia -to-the hydrogen-containing snythesis gas are 'known. These processes havebeen effected at both atmospheric'an'd elevated pressures. tainihg compounds consisting chiefly of primary-amines, are present-in the synthesis productsobtained when Alcohols and other oxygen-containing compounds, however, are only formed in very small amounts.

One object of this invention is the catalytic hydrogena- "tion' of "carbon monoxide with the production of primary synthesis products containing nitrogen-containingcompounds in addition =to"a relatively highcontent :ofoxygencontaining compounds and."prefera'bly' alcohols. This, *and still further objects will become apparent .from the following description:

It has now been found that 'with'the use of special catalysts and synthesis gas containing small quantities :of

gaseous alkaline'reacting compounds, primary products "maybe obta'ined 'with a high content 'of oxygen-conta'ining com ounds, olefins, and nitrogen-containingmoonip'dun'ds.

The hydrogenation is eflected '*at=-'pressures'- of about 1 to 100 atmospheres, andpreferably at pressures of 5 to 40 atmospheres with synthesis gases which contain "about "0.5 to approximately 6 pa'rts by volume of' hydrogen for each'part by volume ofcarbon monoxide and small quantities, preferablyOLS to--2% or alkaline-reactingfcompoun'ds gaseous under synthesis'conditions ai' ud preferably ammonia or derivatives-"thereof, such to instance 'n'iethyl'amine. The synthesis is effected" t t'em- .perat'ures of about 170 'to 300 C. and preferablyat temperatures of 190m 260 C.

The catalysts 'used in accordance with "the invention are'precipitatediron catalysts which are free' fromor 'jcoii't'ain relati'velysmall quantities of carrier materials. Ki eselguhr' and activated bleaching earthhaveproven "particularlygood' as carrier material of't'his kind. Not 'more' than 25% by weight, and preferably less than by weight of carriermaterial should'be present in relation to -the"iron in the catalyst. The catalyst-mustbe reduced'in accordance with the inventionto a' free iron content of. more than 60 and'preferably more than.80% of the total iron content. Reduction is effected withreduction gases such as, for example,- carbommonoxido and/or hydrogen. The catalyst may be activated, it nec- A certain amount of nitrogen-,con-

2,821,537 Patented Jan. 28, 19.5

2 essary or desired, with copper, .silver, .or metals of the second to seventh group of .theperiotlic system. From these .metals, :the metals .of groupll of the-periodic classification, but :also .the metals .titanium, vanadium, .cerium, -5 thoriumandmanganeselhave successfully been used.

The catalyst must be .prepared by precipitation from "an aqueous solution .under alkaline conditions at preferably a .pH ofabout 8 .to .10. The precipitated catalyst .must have .a content-ofalkali oxide .of between 1 ,and

10 1 5% and preferably between .5 .and 10% calculated'as K 0 and based on .the .iron present. The final alkali oxidecontentmay be obtained by totally washing the precipitated catalyst and thereafter. impregnatingthe .catalyst with alkali oxide or'by partially washing the precipi- -t-ated catalyst to the-alkali oxide content desired. Also a combination of these -two expedients .is .possible.

If :an increased yield of .estersrather than alcohols is desired, inaccordance withtheinvention, the catalyst should be impregnatedeither, partially orexclusively with salts of non-volatile acids, such as,.for example, alkali phosphates; borates, and tungstates. Also in this case/the alkali iswadded in quantities of between 1 and 15%, calculated as K 0. If alcohols preferably are desired, the

alkali --may .be introduced into thecatalyst in the form of :a salt ofavolatileoacid, ofzanaacid which decomposes during the reduction, or -.in the-form of vthe hydroxide.

:Ithas been-.foundgthat the lifezand activityv of .the. iron catalyst used in accordance with-the invention may .be increased-if theyare-dried 'pI'-lO1MtO reduction atatem- -perature offimto=150 C,, and; preferably 110 C. to..a

residual water content of 4 to 1% by weight of H 0.

Gatalysts reduced from suitable oxygen-containing compounds withtreducing gasesat-linear, gas velocities of. at

least to 50 cm. per second, preferably 100 to 200cm.

'cper-asecond,measured-in the cold'state (0C.; 760 mm.

" I-1 g) and'rtemperatures -of approximately 200 to 400 C. W.r67vfOlmd lO be;,-particularly active. For this reduction, irtheense :ofvreduction gases rich ;in carbon monoxide has ubeent foundv particularly -favorable under certain circum- 4 stances. The reduction-maybeetfected even with pure carbon monoxide. In general, acarbon monoxide to bydrogenproportion by volume of l 1 to 1:2;is satisfactory. The usei'of carbon monoxide or; gases containing carbon :monoxide. during'the reduction :is .of advantage especially i'mcases wherewa high reduction value-along with lowest possible reductiontemperatures .is desirable.

If the catalysts have-a copper contentof more ,than 115% and preferably between 15 and,,50%, a particularly high formation of oxygen-containing products will be eifected,

t .and the synthesis-may ,be carried out atrelatively-low .tem-

aperatures.

This result-.1 is also. obtained: by psi-rig catalysts ;havipg ia grain size avhichisrbelow 2mm, in diameterzandupref- :erably 'between':0.5 land 1.5. .mm; in :diametenand asvnni- "form'tias possible. With rrespect to the uniformity 1a tolerance ofsapproxirnately 1 0.3 .is 1 allowed. tWith the use of 'th'ese -catalystsg it has :been found particularly advantageous un'der' certain circumstances to etfectathe synthesis with synthesis gases which are conducted from ing'of 'the' pressure loss is possible in this away.

ln the past'it'has only 'very rarely been possible to "-'p'recipitate catalysts from-=siilfate-solutions. However, in accordance with the -invention,'-the catalyst may be pre- 'cipitated 5 from 's'u'lfate solutions with approximately 10 .70 -"to 50% and preferablyapproximately"25* to 30%"of' the iron present being converted into thetrivalent-form. "The washing of the precipitated mass obtained should be carried out with the use of ion exchanging compounds and preferably the use of easily soluble ammonia compounds. The washing, predrying and drying must be expediently eflected with the abundant admittance of air in order to obtain a further oxidation of the bivalent iron still present to convert the same into the trivalent 'form. In any case, more than 70% and preferably more than 80% of the total iron in the catalyst should be present in the trivalent form before the reduction. It is of advantage to increase the concentration of the ion exchanging compounds in the washing water during the washing in order to obtain a maximum washing with small quantities of water. In general, washing waters are preferably used with a content of ion exchanging compounds of 0.2 to 20% and preferably of 0.2 to 2%. The individual steps to be taken for the precipitation of the catalysts from sulfate solutions are the same as stated in patent application Serial No. 280,173, filed April 2, 1952, now Patent No. 2,786,817.

The synthesis itself should be elfected in a manner which assures careful treatment of the catalyst, with straight gas passage and preferably with recycling of the synthesis gas, using 1 to 10 parts and preferably 3 to 5 parts by volume of recycled gas for each part by volume of fresh synthesis gas.

The gas load should generally be about 1,000 volumes of fresh gas per volume of catalyst per hour, preferably 100-500 volumes.

The use of a temperature gradient, i. e., an increasing catalyst temperature in the direction of gas flow, is of advantage in special cases. This is true, for example, if in a synthesis carried out with once-through operation or with only little gas recycling, as, for example, 1 volume of fresh gas+0.5 volume of recycle gas, the concentration between the inlet and the outlet of the reactor becomes considerably lower so that an increased temperature at the reactor outlet as compared with that at the reactor inlet is favorable for increasing the rate of conversion at the reactor outlet.

It is possible to effect the synthesis in accordance with the invention, using a fixed catalyst bed, a liquid phase synthesis or a fluidized process. When working with the fluidized bed process, the synthesis is effected in a gaseous phase with a finely distributed catalyst layer, particles of which are eddying in a lively whirling motion, thus forming a fluidized bed.

The carbon monoxide hydrogenation products obtained in accordance with the invention, have a content of more than oxygen-containing compounds in addition to more than 10% of amines and a high content of olefins.

The following examples are given to illustrate the invention and not to limit the same:

Example 1 A catalyst was precipitated from a boiling solution containing 40 gms. of iron and 12 gms. of copper per liter by pouring the solution into a boiling soda solution containing 101 gms. of soda per liter. The pH was 9.2. The filtered catalyst mass was freed from excess alkali by repeated washing with condensate and then impregnated with potassium carbonate in such a manner that 8 parts by weight of potassium carbonate calculated as K 0 for 100 parts by weight of iron were present. The grain size of the dried and molded mass was between 1 and 3 mm.

The reduction was carried out at a temperature of 320 C. with the use of a gas mixture consisting of 75% of hydrogen and of nitrogen at a linear gas velocity of 1.4 meters per second. The reduction time was 120 minutes, the reduction value was 65% of metallic iron.

When water gas containing 2% of NH was passed over this catalyst at a pressure of atmospheres, and a gas load of 100 liters of gas per liter of catalyst per hour, a conversion rate of 56% of CO+H was obtained at a temperature of 183 C.

The processing of the synthesis product obtained yielded 35% of oxygen-containing compounds consisting chiefly of primary aliphatic alcohols, in addition to 17% of nitrogen-containing compounds consisting chiefly of primary aliphatic amines. The olefinic portion in the remaining hydrocarbons was 60% in the gasoline boiling range and 50% in the diesel oil boiling range.

When the same catalyst was charged with twice the gas quantity, a CO-i-H conversion of 50% could be obtained at a temperature of 196 C.

When charging the catalyst with three times the gas quantity, a CO+H conversion of 55% was obtained at a temperature of 210 C.

The yield of nitrogen-containing and oxygen-containing products was slightly reduced under these conditions.

Example 2 An aqueous solution of iron nitrate and copper nitrate of the concentration as mentioned in Example 1 was poured into a boiling soda solution containing gms. of Na CO per liter. After filtration, the precipitated catalyst slurry was partially washed with hot condensate so that finally 8 parts of alkali calculated as K 0 and based on 100 parts of iron remaining in the catalyst. The mass was molded, dried at a tempearture of C., and sieved to a grain size of between 1.5 and 3 mm.

The reduction was carried out for 90 minutes at a temperature of 310 C. with hydrogen at a linear gas velocity of 1.5 in. per second, measured in the cold state. The reduction value was 70% of metallic iron.

Water gas containing 2% of NH was passed over the catalyst at a pressure of 30 atmospheres, a temperature of C. and a gas load of 100 liters of gas per liter of catalyst per hour. The CO+H conversion was 60%.

Working up the synthesis product yielded 39% of oxygen-containing compounds, chiefly primary aliphatic alcohols, in addition to 15% of nitrogen-containing compounds consisting chiefly of primary amines.

Example 3 A catalyst was prepared in the manner described in Example 1. The ratio of iron to copper was 100 to 10. The reduction value was 80% of metallic iron. The impregnation was effected with the use of primary potassium phosphate in such a manner that 8 parts of potassium phosphate calculated as K 0 for every 100 parts of Fe were present in the catalyst. Under the reduction and synthesis conditions of Example 1, a CO+H conversion of 53% was obtained at a gas load of 100 liters of gas per liter of catalyst per hour. The proportion of nitrogencontaining compounds and preferably of primary aliphatic amines, was 12% in addition to 30% of oxygen-containing compounds consisting chiefly of aliphatic alcohols.

Example 4 A solution consisting of iron sulfate and copper sulfate and containing 5 parts of copper for every 100 parts of iron and having a concentration of 40 parts of iron for every 1000 parts of water was heated until it boiled and precipitated in the hot state by pouring it into a soda solution of 80 C. containing 90 gms. of Na CO per liter. During the precipitation, an air stream was blown through the precipitation apparatus. The quantity of air was 600 liters for every 25 gms. of iron, the blowing time being 3.5 minutes. Immediately thereafter, the precipitate was freed from the mother liquor by subjecting it to a suction filtration and was then washed two times with a quantity of boiling condensate corresponding to twelve times the quantity of iron present. Finally, the catalyst mass was washed three times by suspending it in an ammonium carbonate solution containing 5 to 10 gms. of ammonium carbonate dissolved in 1500 cc. of solution. 1500 cc. of washing solution for every 25 gms. of iron were used in each of the three washings. After the last washing, the sulfur content in the finished catalyst was only 0.02%.

28% of the total Fe were now present as Fe(III), the balance being Fe(II). Then the catalyst mass was impregnated in a potassium carbonate solution in such a manner that 8 parts of alkali calculated as K 0 for every 100 parts of iron were contained in the mass.

The catalyst mass was dried for 24 hours at a temperature of 110 C. with circulating air and crushed to a grain size of 2-4 mm. The content of Fe(III) was now 88%. Thereafter, the catalyst was reduced for 1 hour at a temperature of 300 C., using a gas mixture consisting of 75% of hydrogen and 25% of nitrogen at a linear gas velocity of 1.4 meters per second, measured in the cold state. Thereafter, the reduction value of the catalyst was 68% of free iron.

A gas consisting of35 parts of CO, 55 parts of H 2% of ammonia, the balance being carbon dioxide, nitrogen and methane, was passed over this catalyst at a gas load of 100 liters of gas per liter of catalyst per hour, a synthesis pressure of 30 atmospheres and a synthesis temperature of 192 C. A CO+H conversion of 65% was obtained. The resulting product was worked up yielding 33% of oxygen-containing compounds consisting chiefly of primary aliphatic compounds, in addition to 13% of nitrogen-containing compounds consisting chiefly of primary amines.

I claim:

1. In a process for the catalytic hydrogenation of carbon monoxide, the improvement which comprises intimately contacting under conditions of temperature between 170 and 300 C. and at conditions of pressure between about 1 and 100 atmospheres, a carbon monoxide hydrogenation synthesis gas containing 0.5 to 6 parts by volume of hydrogen per each part by volume of carbon monoxide and 0.5 to 2% by volume of a member selected from the group consisting of ammonia and methylamine with a precipitated iron catalyst which has been reduced to a free iron content of more than 60% and containing 0 to 25% of a carrier material and about 1 to 15% alkali oxide calculated as K 0 and based on the iron present, and recovering the carbon monoxide hydrogenation product with more than 20% oxygen containing compounds, more than 10% amines and with a high content of olefins.

2. Improvement according to claim 1, in which said contacting is effected at a pressure of about 10 to 30 atmospheres.

3. Improvement according to claim 1, in which said catalyst has an alkali oxide content of about 5 to 10% calculated as K 0.

4. Improvement according to claim 1, in which said catalyst is impregnated with a salt of a non-volatile acid in order to obtain said alkali content.

5. Improvement according to claim 4, in which said salt is a non-volatile acid selected from the group consisting of alkali phosphates, alkali borates and alkali tungstates.

6. Improvement according to claim 1, in which said catalyst has a copper content in excess of 15%.

7. Improvement according to claim 1, in which said catalyst has a substantially uniform grain size below 2 mm. in diameter.

8. Improvement according to claim 1, in which said catalyst is a catalyst precipitated from a sulfate solution with about 10 to of the iron present converted into the trivalent form, washed with ion exchanging solutions, predried and dried, said washing, predrying and drying being effected with a further oxidation of the residual bi valent iron to more than a trivalent iron content.

References Cited in the file of this patent UNITED STATES PATENTS 2,133,267 Ayers Oct. 18, 1938 2,374,454 Oliver et a1 Apr. 24, 1945 2,422,631 Olin et a1 June 17, 1947 2,438,584 Stewart Mar. 30, 1948 2,449,071 Hawk et al Sept. 14, 1948 2,483,512 Voorhies et al. Oct. 1, 1949 2,518,754 Clark Aug. 15, 1950 2,560,970 Martin July 17, 1951 2,727,056 Gross et a1. Dec. 13, 1955 FOREIGN PATENTS 672,405 Great Britain May 21, 1952

Claims (1)

1. IN A PROCESS FOR THE CATALYST HYDROGENATION OF CARBON MONOXIDE, THE IMPROVEMENT WHICH COMPRISES INTIMATELY CONTACTING UNDER CONDITIONS OF TEMPERATURE BETWEEN 170 AND 300*C. AND AT CONDITIONS OF PRESSURE BETWEEN ABOUT 1 AND 100 ATMOSPHERES, A CARBON MONOXIDE HYDROGENATION SYNTHESIS GAS CONTAINING 0.5 TO 6 PARTS BY VOLUME OF HYDROGEN PER EACH PART BY VOLUME OF CARBON MONOXIDE AND 0.5 TO 0% BY VOLUME OF A MEMBER SELECTED FROM THE GROUP CONSISTING OF AMMONIA AND METHYLAMINE WITH A PRECIPITATED IRON CATALYST WHICH HAS BEEN REDUCED TO A FREE IRON CONTENT OF MORE THAN 60% AND CONTAINING 0 TO 25% OF A CARRIER MATERIAL AND ABOUT 1 TO 15% ALKALI OXIDE CALCULATED AS K2O AND BASED ON THE IRON PRESENT, AND RECOVERING THE CARBON MONOXIDE HYDROGENATION PRODUCT WITH MORE THAN 20% OXYGEN CONTAINING COMPOUNDS, MORE THAN 10% AMINES AND WITH A HIGH CONTENT OF OLEFINS.